Process for manufacturing ethyleneamine compounds

ABSTRACT

The present disclosure pertains to a process for manufacturing ethyleneamine compounds selected from the group of ethyleneamines and hydroxyethylethyleneamines wherein the process comprises two reaction sequences.

CROSS-REFERENCE TO RELATED APPLICATION

This application is a U.S. National-Stage entry under 35 U.S.C. § 371 based on International Application No. PCT/EP2020/053751, filed Feb. 13, 2020 which was published under PCT Article 21(2) and which claims priority to European Application No. 19156902.9, filed Feb. 13, 2019, which are all hereby incorporated in their entirety by reference.

TECHNICAL FIELD

The present disclosure pertains to the manufacture of ethyleneamine compounds selected from the group of ethyleneamines, and hydroxyethylethyleneamines.

BACKGROUND

Ethyleneamine compounds, more specifically ethyleneamines and hydroxyethylethyleneamines, are useful in many applications.

Ethyleneamines consist of two or more nitrogen atoms linked by ethylene units. Ethyleneamines can be present in the form of linear chains H2N(—CH2-CH2-NH)p-H. For p=1, 2, 3, 4, . . . this gives, respectively, ethylenediamine (EDA), diethylenetriamine (DETA), present disclosure linear triethylenetetramine (L-TETA), and linear tetraethylenepentamine (L-TEPA). As will be clear, this range can be extended. With three or more ethylene units it is also possible to create branched ethyleneamines such as N(CH2-CH2-NH2)3, trisaminoethylamine (TAEA). Two adjacent nitrogen atoms can be connected by two ethylene units to form a piperazine ring. Piperazine rings can be present in longer chains to produce the corresponding piperazine-ring-containing ethyleneamines.

Ethyleneamines, in particular diethylenetriamine (DETA) and further higher ethyleneamines such as linear triethylenetetramine (L-TETA) and linear tetraethylenepentamine (L-TEPA), are attractive products from a commercial point of view. In particular, the interest in higher ethyleneamines is increasing as these compounds have numerous commercial applications, e.g., as starting materials for, or use in, asphalt additives, corrosion inhibitors, epoxy curing agents, fabric softeners, fuel additives, hydrocarbon purification, ion exchange resins, lube oil additives, paper wet-strength resins, petroleum production chemicals, solvents, synthetic resins such as amide resins, mineral processing aids and interface-active substances (surfactants).

Hydroxyethylethyleneamines find application in chemical processes, as solvent or as reactant. For example, aminoethylethanolamine or AEEA of the formula H2N-CH2-CH2-NH-CH2-CH2-OH is an organic base used in the industrial manufacture of fuel and oil additives, chelating agents, and surfactants. Chain-extended ethanolamines, e.g., monoethanolamine compounds of the formula H2N—(CH2-CH2-NH)q-CH2-CH2-OH, wherein q is 2 or higher, are interesting intermediates for various types of organic synthesis, e.g., the manufacturing of esters of carboxylic acids. They can also be used in, for example, the formation of synthetic resins, as surfactants, for the production of emulsifiers, in fabric softeners, and as epoxy curing agents.

Today, the EDC-based process is the main process for producing higher ethyleneamines, defined for the purposes of the present specification as ethyleneamines with at least two ethylene moieties. The EDC route is the substitution reaction of EDC (ethylenedichloride) with ammonia and/or an ethyleneamine at elevated temperatures and pressures to form hydrochloride salts of ethyleneamines which are then reacted with caustic to generate mixtures of ethyleneamines and NaCl. The EDC route has its disadvantages. It is dependent on the use of ethylenedichloride which is expensive, difficult to handle, and connected to HSE issues. Additionally, the EDC route gives a mixture of many different ethyleneamines Nevertheless, as demonstrated by its widespread use, it remains an attractive process for manufacturing ethyleneamines.

In view of the fluctuating market conditions for ethyleneamine compounds and for the starting materials used in their manufacture there is need in the art for a process which allows flexibility in the products produced, and in the starting materials used. There is also need in the art for a process which combines flexibility for the starting materials and products used with efficient use of apparatus and efficient processing of waste streams.

The present disclosure provides a process which addresses these issues. In addition, other objects, desirable features and characteristics will become apparent from the subsequent summary and detailed description, and the appended claims, taken in conjunction with the accompanying drawings and this background.

BRIEF SUMMARY

This disclosure provides a process for manufacturing ethyleneamine compounds selected from the group of ethyleneamines and hydroxyethylethyleneamines, wherein the process comprises a first and a second reaction sequence,

the first reaction sequence comprising the steps of:

-   -   in an adduction step, providing a CO2 adduct of a starting         compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH         moiety, or HO—CH2-CH2-OH,     -   in a chain-extension step, reacting a hydroxy-functional         compound selected from ethanolamines and dihydroxyethane with an         ethyleneamine compound, wherein at least part of a total of         hydroxy-functional compounds and the ethyleneamine compound is         provided in the form of a CO2 adduct, to form a CO2 adduct of a         chain-extended ethyleneamine compound,     -   in an elimination step, converting the CO2 adduct of the         chain-extended ethyleneamine compound to the corresponding         product ethyleneamine compound by removal of the carbonyl group,         and

the second reaction sequence comprising the steps of:

-   -   in a ethylenedichloride reaction step, reacting         ethylenedichloride with at least one compound selected from the         group of ammonia, an ethyleneamine and/or an ethanolamine to         form a hydrochloride salt of the ethyleneamine and/or the         ethanolamine,     -   in a caustic treatment step, reacting a hydrochloride salt of         the ethyleneamine or ethanolamine with a base to form an         ethyleneamine compound and an inorganic chloride salt,     -   in a salt separation step, separating the inorganic chloride         salt from the ethyleneamine compound,         wherein the first reaction sequence and the second reaction         sequence are connected in that at least one of the following         takes place:     -   effluent from a step in the first reaction sequence is provided         as a starting material to a step in the second reaction         sequence,     -   effluent from a step in the second reaction sequence is provided         as a starting material to a step in the first reaction sequence,     -   a step of the first reaction sequence and a step of the second         reaction sequence are combined, or     -   effluent from a step in the first reaction sequence is combined         with effluent from a step in the second reaction sequence.

BRIEF DESCRIPTION OF THE DRAWINGS

The present disclosure will hereinafter be described in conjunction with the following drawing figures, wherein like numerals denote like elements, and:

FIG. 1 illustrates a first embodiment of the process as contemplated herein.

FIG. 2 further embodiments of the process as contemplated herein.

FIG. 2a illustrates further embodiments of the process as contemplated herein.

FIG. 3 illustrates a further embodiment of the process as contemplated herein.

FIG. 4 illustrates a further embodiment of the process as contemplated herein.

FIG. 5 illustrates a further embodiment of the process as contemplated herein.

FIG. 6 illustrates a further embodiment of the process as contemplated herein.

DETAILED DESCRIPTION

The following detailed description is merely exemplary in nature and is not intended to limit the disclosure or the application and uses of the disclosure. Furthermore, there is no intention to be bound by any theory presented in the preceding background of the disclosure or the following detailed description.

The present disclosure pertains to a process for manufacturing ethyleneamine compounds selected from the group of ethyleneamines and hydroxyethylethyleneamines wherein the process comprises two reaction sequences, the first reaction sequence comprising the steps of

in an adduction step providing a CO2 adduct of a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH,

in a chain-extension step reacting a hydroxy-functional compound selected from ethanolamines and dihydroxyethane with an ethyleneamine compound, wherein at least part of the total of hydroxy-functional compounds and ethyleneamine compound is provided in the form of a CO2 adduct, to form a CO2 adduct of a chain-extended ethyleneamine compound,

in an elimination step converting a CO2 adduct of a chain-extended ethyleneamine compound to the corresponding product ethyleneamine compound by removal of the carbonyl group, and

the second reaction sequence comprising the steps of

in a ethylenedichloride reaction step reacting ethylenedichloride with at least one compound selected from the group of ammonia, an ethyleneamine and/or an ethanolamine to form a hydrochloride salt of an ethyleneamine and/or ethanolamine,

in a caustic treatment step reacting the hydrochloride salt of an ethyleneamine or ethanolamine with a base to form ethyleneamine compound and an inorganic chloride salt,

in a salt separation step separating the inorganic salt from the ethyleneamine compound, with the first reaction sequence and the second reaction sequence being connected in that at least one of the following takes place:

effluent from a step in the first reaction sequence is provided as starting material to a step in the second reaction sequence,

effluent from a step in the second reaction sequence is provided as starting material to a step in the first reaction sequence,

a step of the first reaction sequence and a step of the second reaction sequence are combined, or

effluent from a step in the first reaction sequence is combined with effluent from a step in the second reaction sequence.

The process as contemplated herein uses two connected reaction sequences for the manufacture of ethyleneamine compounds. Each reaction sequence has its own advantages. The process of the first reaction sequence allows the manufacture of high molecular weight ethyleneamine compounds, in particular straight-chain compounds. The process of the second reaction sequence allows the manufacture in an efficient manner of a reaction product comprising a mixture of many different ethyleneamine compounds, some of which are interesting as products in themselves while others may be more attractive as starting materials for the manufacture of higher ethyleneamine compounds. As will be discussed in more detail below, the process as contemplated herein allows for flexibility in starting materials used and products produced, and an efficient use of apparatus.

In some embodiments, the process as contemplated herein makes it possible to use products from one reaction sequence as starting material in another reaction sequence, therewith allowing the manufacture of desirable products in an efficient manner. In other embodiments, the process as contemplated herein makes for the possibility of combined product work-up and waste treatment, which is an efficiency measure.

Further advantages of the present disclosure and specific embodiments thereof will become apparent from the further specification.

In the following, the two individual reaction sequences will be discussed. Then, the various ways in which the reaction sequences can be connected will be discussed.

The first reaction sequence

The first reaction sequence comprises the steps of

in an adduction step providing a CO2 adduct of a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH,

in a chain-extension step reacting a hydroxy-functional compound selected from ethanolamines and dihydroxyethane with an ethyleneamine compound, wherein at least part of the total of hydroxy-functional compounds and ethyleneamine compound is provided in the form of a CO2 adduct, to form a CO2 adduct of a chain-extended ethyleneamine compound,

in an elimination step converting a CO2 adduct of a chain-extended ethyleneamine compound to the corresponding product ethyleneamine compound by removal of the carbonyl group.

Starting materials for the first reaction sequence are a hydroxy-functional compound selected from ethanolamines and dihydroxyethane, and an ethyleneamine compound. The core of the first reaction sequence is that a hydroxy-functional compound reacts with an amine-functional compound with conversion of a primary amine into a secondary amine or a secondary amine into a tertiary amine. For example, a compound exemplified by formula R—OH may react with a compound exemplified by the formula H2NR′, to form a compound exemplified by the formula R—NH—R′, with formation of water. For a further example, a compound exemplified by formula R—OH may react with a compound exemplified by the formula RNR′ R″, with formation of water.

Hydroxyl-functional compounds are selected from the group of ethanolamines and dihydroxyethane. In the context of the present specification, the group of ethanolamines encompasses 2-hydroxy-ethylamine, also indicated as monoethanolamine or MEA, and hydroxyethylethyleneamines. Preferred hydroxy-functional compounds include monoethanolamine (MEA), aminoethylethanolamine (AEEA), hydroxyethyl-diethylenetriamine (HE-DETA), hydroxyethyltriethylenetetraamine (HE-TETA), and diethanolamine

The hydroxyl-functional compound is reacted with an ethyleneamine compound. Ethyleneamine compounds comprise at least one —NH2 group. Preferred ethyleneamine compounds include ethylenediamine (EDA), N-methylethylenediamine (MeEDA), diethylenetriamine (DETA), piperazine (PIP), N-aminoethylpiperazine (AEP), triethylene tetramine (TETA), N, N′-diaminoethylpiperazine (DAEP), tetraethylenepentamine (TEPA), and pentaethylenehexamine (PEHA).

Ethyleneamine compounds may also encompass ethanolamines as described above. If an ethanolamine is used as ethyleneamine compound, the first reaction sequence will result in the formation of (chain-extended) hydroxyethylethyleneamines. If it is desired to manufacture ethyleneamines, the ethyleneamine compound to be reacted with the hydroxyl-functional compound should not be an ethanolamine, but selected from ethyleneamines that do not contain a hydroxy group.

Some structures of ethyleneamines and hydroxy-functional compounds are provided below:

Preferred examples of product polyethyleneamine compounds are triethylene tetramine (TETA), N,N′-diaminoethylpiperazine (DAEP), tetraethylenepentamine (TEPA), pentaethylenehexamine (PEHA), N-[(2-aminoethyl) 2-aminoethyl]piperazine) (PEEDA), and 1-[2-[[2-[(2-aminoethyl)amino]ethyl]amino]ethyl]piperazine) (PEDETA).

Adduction Step

The first step in the first reaction sequence of the present disclosure is an adduction step, in which a CO2 adduct is provided of a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH. The adduction step can be carried out in various manners.

In one embodiment, the adduction step comprises the step of reacting gaseous CO2 with a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH, resulting in the formation of the respective CO2 adducts. This step is also indicated herein as the absorption step.

In another embodiment of the adduction step, the CO2 adduct is formed by reaction of a starting compound comprising —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH with a compound not being CO2 which can transfer a carbonyl group to the starting compounds, resulting in the formation of CO2 adducts thereof. These compounds can be indicated as carbon oxide delivering agents.

Carbon oxide delivering agents other than CO2 within the scope of the present disclosure include organic compounds in which a carbonyl moiety is available for being transferred as described above. Organic compounds in which a carbonyl moiety is available include urea and derivatives thereof; linear and cyclic ethylene ureas, especially cyclic ethylene urea, mono or di-substituted ethylene ureas, alkyl and dialkyl ureas, linear and cyclic carbamates, organic carbonates and derivatives or precursors thereof. Such derivatives or precursors may for example include ionic compounds such as carbonate or bicarbonate salts, carbamic acids and associated salts, that can be converted, in some embodiments in situ in the process of the present disclosure, into their non-ionic counterparts, for example into linear and cyclic carbamate or urea compounds. When such ionic compounds are used in the present disclosure, they are organic hydrocarbon-based carbonate, bicarbonate or carbamate salts. Preferably the CO delivering agent is CO2 or an organic compound that is suitable for use as a carbon oxide delivering agent, or urea or ethylene carbonate, more preferably the carbon oxide delivering agent is at least partly added as carbon dioxide or urea. The carbon oxide delivering agent can be present in the process in the same molecule as the amine functional or the ethanolamine functional compound by using the aforementioned urea or carbamate compounds.

Examples of carbon oxide delivering agents include

In the above drawing CAEEA again stands for the cyclic carbamate of aminoethylethanolamine, UDETA for the urea of diethylene triamine, DAEU stands for diaminoethyl urea, AE AE carbamate stands for amino ethyl aminoethanol carbamate, CHE-DETA stands for the carbamate of hydroxyethyldiethylene triamine, U1TETA stands for the terminal urea of triethylene tetramine, and DUTETA stands for the 1,3-diurea of triethylene tetramine

The carbon oxide delivering agent is most preferably added to the reaction in the form of carbon dioxide, urea, the carbamate derivative of the ethanolamine-functional compound or the urea derivative of the ethyleneamine compound, or a combination of these. Examples include CMEA, EU, UDETA, and UAEEA, which is the CO2 adduct of aminoethylethanolamine

The embodiment of the adduction step in which the CO2 adduct is formed by reaction of a starting compound comprising —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH with a compound not being CO2 which can transfer a carbonyl group to the starting compounds, can also be indicated as a CO2 transfer step.

In a preferred embodiment of the present disclosure, the adduction step is an absorption step in which CO2 is absorbed in a reaction medium comprising a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH to form a CO2 adduct of said starting compound and the elimination step is a desorption step in which the CO2 adduct of the product polyethyleneamine compound is reacted with water to form the corresponding ethyleneamine compound and CO2.

Absorption Step

In the absorption step carried out in one embodiment of the process as contemplated herein, CO2 is absorbed in a reaction medium comprising a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH to form a CO2 adduct of said starting compound. CO2 adducts of these compounds thus include compounds which a —NH—CH2-CH2-NH— moiety is converted to a urea moiety in which two nitrogen atoms are connected via a carbonyl moiety and an ethylene moiety, in accordance with the following formula:

CO2 adducts also include cyclic carbamate compounds

CO2 adducts also include compounds in which the HO—CH2-CH2-OH is converted to a ethylenecarbonate molecule which the two 0-atoms of HO—CH2-CH2-OH are connected through via a carbonyl moiety and an ethylene moiety.

In the above, the CO2 adducts are presented as adducts formed by reaction within a single molecule. Of course, CO2 adducts can also be formed by reaction of reactive groups of different molecules. Within the context of the present specification a CO2 adduct moiety is in many embodiments a moiety wherein two nitrogen atoms, or a nitrogen atom and an oxygen atom, or two oxygen atoms, are connected through a —C(O)— moiety. Furthermore CO2 adducts can also form with a single amine or alcohol in a terminal single sided group, i.e. they can be adducts linked to only one nitrogen or oxygen atom.

The absorption step is carried out by contacting CO2 with a reaction medium comprising a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH to form a CO2 adduct. The contacting step is to be carried out under such conditions that CO2 is absorbed and that a CO2 adduct is formed.

Reaction conditions include a reaction temperature which generally is at least about 120° C. At a temperature below about 120° C., the reaction rate generally is too low to allow meaningful conversion within a reasonable time frame. It may be preferred for the reaction temperature to be at least about 140° C., in particular at least about 150° C., more in particular at least about 170° C. The reaction is generally carried out at a temperature of at most about 400° C. The temperature may thus be at most about 300° C., in particular at most about 250° C., or even at most about 220° C. Operating at a temperature of from about 170-about 220° C. is considered preferred.

The pressure during the reaction is determined for the major part by the provision of CO2 to the reaction medium, with the total pressure in the system decreasing during the reaction due to the consumption of CO2. In general, the total pressure in the system is at most about 75 bara. The total pressure generally is at least about 2 bara, in particular at least about 5 bara, more in particular at least about 10 bara.

The amount of CO2 provided to the reaction is not critical. The minimum amount is governed by the amount required to convert the starting material amine compound into its corresponding CO2 adduct. Therefore, the molar ratio between CO2 and —NH—CH2-CH2-NH— moieties, —NH—CH2-CH2-OH moieties, or HO—CH2-CH2-OH generally is at least about 0.1:1. A ratio of at least about 0.2:1, in particular at least about 0.5:1 may be more attractive if more urea adduct is aimed for. A large excess of CO2 is not detrimental to the process, but is generally less attractive for economic reasons. Therefore, as a general maximum a value of about 500:1 may be mentioned. The amount of CO2 dosed will depend on the desired amount of urea adduct in the final product.

In one embodiment, the absorption step is carried out by reacting a compound selected from the group of starting ethyleneamine and hydroxy-functional compounds comprising at least one —NH—CH2-CH2-NH— moiety and at least two ethylene moieties in total, with CO2 in the presence of an auxiliary compound selected from ethylenediamine (EDA), monoethanolamine (MEA) and mixtures thereof, the molar ratio of auxiliary compound to amine compound being at least about 0.02:1.

For the process of this embodiment it is preferred for the ethyleneamine compound to be selected from diethylenetriamine (DETA), triethylenetetramine (L-TETA), aminoethylethanolamine (AEEA), and hydroxyethyldiethylenetriamine (HE-DETA). It is preferred for the molar ratio of auxiliary compound to amine compound to be at least about 0.05:1, in particular at least about 0.1:1, and/or at most about 10:1. It is preferred for the reaction to be carried out at a temperature of at least about 120° C., preferably at least about 140° C., in particular at least about 150° C., more in particular at least about 170° C., and/or at most about 400° C., in particular at most about 350° C., more in particular at most about 300° C., still more in particular at most about 250° C. or even at most about 220° C., for example at a temperature of from about 170-about 250° C. or about 170-about 220° C. It is preferred for the molar ratio between CO2 and —NH—CH2-CH2-NH— moieties in the amine compound to be at least about 0.5:1 and/or at most about 500:1. It is preferred for the reaction time to be at most about 10 hours, in particular at most about 6 hours, more in particular at most about 3 hours and/or at least about 5 minutes, in particular between about 0.5 and about 2 hours.

In one embodiment, the absorption step is carried out via a two-step process wherein

in an absorption step a liquid medium comprising an ethyleneamine compound having a linear —NH—CH2-CH2-NH— group is contacted with a CO2-containing gas stream at a pressure of at most about 20 bara, resulting in the formation of a liquid medium into which CO2 has been absorbed,

bringing the liquid medium to CO2 adduct formation conditions, and in a CO2 adduct formation step forming a CO2 adduct of the ethyleneamine compound, the CO2 adduct formation conditions including a temperature of at least about 120° C., wherein the total pressure at the end of the CO2 adduct formation step is at most about 20 bara, wherein the temperature in the absorption step is lower than the temperature in the CO2 adduct formation step.

By separating the CO2 absorption step from the urea formation step in this embodiment the CO2 absorption step can be carried out at relatively low temperatures and pressures. In the absorption step CO2 is absorbed in the liquid reaction medium. In the reaction step the absorbed CO2 is reacted with the ethyleneamine compound to form an cyclic urea adduct. This means that in the urea formation step the provision of further CO2 is not required, and that the absorption step is carried out until sufficient CO2 has been absorbed in the liquid medium to achieve the desired conversion of ethyleneamine compound into cyclic ureas in the urea formation step. As indicated above, the provision of further CO2 to the reaction medium during the urea formation step (in addition to the CO2 provided during the absorption step) is not required, and generally not attractive because it will increase the pressure during the urea formation step. If so desired for some reason, at most about 20% of the total CO2 required to achieve the desired urea conversion is added during the urea formation step, in particular at most about 10%. In one embodiment of this embodiment, the CO2-containing gas stream comprises at least about 95 vol. % of CO2. In another embodiment of this embodiment, the CO2-containing gas stream comprises at most about 70 vol. % of CO2, in particular at most about 60 vol. % of CO2 and above about 0.01 vol. %, in particular between about 4 and about 60 vol. %. It may be preferred for the step of contacting the liquid medium with the CO2-containing gas steam in the absorption step to be carried out at a temperature between about 0° C. and about 200° C., in particular at a temperature of at most about 190° C., more in particular at most about 150° C., or at most about 130° C., more in particular at most about 110° C. and preferably at a value of at least at least about 20° C., in particular at least about 40° C. It may be preferred for the maximum total pressure in the absorption step to be between about 1 and about 15 bara, more in particular between about 1 and about 10 bara, even more in particular between about 1 and about 3 bara. It may be preferred for the temperature in the urea formation step to be at least about 140° C., in particular at least about 150° C., more in particular at least about 170° C. and preferably at most about 400° C., in particular at most about 300° C., more in particular at most about 250° C., or even at most about 220° C. The urea formation step is preferably carried out in a closed vessel. It may be preferred for the urea formation step to be carried out in a vessel wherein the volume of the liquid medium in the vessel makes up at least about 50% of the total volume of the vessel (including head space), in particular at least about 70%, more in particular at least about 85%. It may be preferred for the pressure at the end of the cyclic urea formation step is below about 15 bara, in particular below about 10 bara, in some embodiments below about 5 bara, or even below about 3 bara.

CO2-Transfer Step

In one embodiment the adduction step comprises a CO2 transfer step. In a CO2 transfer step, a carbonyl group is provided from a CO source to a starting compound comprising a

NH-CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH in an adduction step providing a CO2 adduct of a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH. The CO sources have been discussed above.

Reaction conditions include a reaction temperature which generally is at least about 100° C. At a temperature below about 100° C., the reaction rate generally is too low to allow meaningful conversion within a reasonable time frame. It may be preferred for the reaction temperature to be at least about 125° C., in particular at least about 150° C., more in particular at least about 170° C. The reaction is generally carried out at a temperature of at most about 400° C. The temperature may thus be at most about 300° C., in particular at most about 250° C., or even at most about 220° C. Operating at a temperature of from about 170-about 220° C. is considered preferred.

In general, the total pressure in the system is at most about 75 bara. The total pressure generally is at least about 2 bara, in particular at least about 5 bara, more in particular at least about 10 bara.

The amount of CO moieties provided to the reaction is not critical. The minimum amount is governed by the amount required to convert the starting material amine compound into its corresponding CO2 adduct. Therefore, the molar ratio between CO moieties and independent —NH—CH2-CH2-NH— moieties, —NH—CH2-CH2-OH moieties, or HO—CH2-CH2-OH generally is at least about 0.1:1. A ratio of at least about 0.2:1, in particular at least about 0.5:1 may be more attractive if more urea adduct is aimed for. A large excess of CO moieties is not detrimental to the process, but is generally less attractive for economic reasons. Therefore, as a general maximum a value of about 500:1 may be mentioned. The amount of CO moieties dosed will depend on the desired amount of urea adduct in the final product.

Reaction Step

In the reaction step of the process as contemplated herein a hydroxy-functional compound selected from the group of ethanolamines and dihydroxyethane with an ethyleneamine compound, wherein at least part of the total of hydroxy-functional compounds and ethyleneamine compounds is provided in the form of a CO2 adduct, to form CO2 adduct of a product polyethyleneamine compound.

The reaction step is preferably performed at a temperature of at least about 100° C. The temperature should preferably be lower than about 400° C. More preferably the temperature is between about 200 and about 360° C. Even more preferably the temperature is between about 230 and about 340° C. Most preferably the temperature is between about 250 and about 310° C. In embodiments where the ethanolamine-functional compound is monoethanolamine the most preferred temperature range is between about 230 and about 290° C.

The reaction time during the process is in an embodiment between 5 minutes and about 15 hours, preferably between about 0.5 and about 10 hours, more preferably between about 1 and about 6 hours.

It will be clear to the skilled person that an overly long reaction time will be detrimental, not only for process-economical reasons, but also because it may lead to the formation of undesirable high-boiling side products. A too long reaction time can lead to undesirable degradation and color formation.

If any of the starting compounds contains piperazine units

preferably the reaction is performed in a liquid wherein the liquid comprises water as then both the yield and selectivity can be increased. If one or more of the hydroxy-functional compound, ethyleneamine compound or carbon oxide delivering agent are liquid at the reaction conditions, these are not considered part of the above liquid in which the process of the present disclosure is performed.

In a preferred embodiment when having compounds with piperazine units in the process of the present disclosure, the liquid contains at least about 50 wt % of water up to about 100 wt % of water, wherein more preferably the remaining up to about 50 wt % is a polar liquid that mixes homogenously with water at the conditions employed during the process of the present disclosure. Even more preferably the liquid contains at least about 75 wt-% of water, yet more preferably at least about 90 wt-%, most preferably at least about 95-wt % on total liquid weight.

The reactor employed can be any suitable reactor including continuously stirred tank reactor, pipeline reactor, tubular or multi-tubular reactor. The reactor may be adiabatic or equipped with external or internal heating devices. Feed may be single point or split into multiple points. It can consist of or include multiple stages with inter-stage heat exchange.

As will be clear to the skilled person, the apparatus used in the reaction step, but also in the various other steps of the process as contemplated herein, should be fit for purpose. That is, they should be able to withstand the long-time interaction with the reactants and products under reaction conditions, including, as described elsewhere, substantial temperatures and pressures. In addition to the reactor and other apparatus being able to withstand the reaction conditions, it is also important that they do no release material which would detrimentally affect the quality of the product produced. For example, as metal ions may result in color formation in the product, the material of construction for the various apparatus should be selected such that metal ions are not released to an unacceptable extent. Suitable materials include, but are not limited to, high quality steels such as austenitic stainless steels, super austenitic stainless steels, ferritic stainless steels, martensitic stainless steels, precipitation-hardening martensitic stainless steels, and Duplex stainless steels. It is within the scope of the skilled person to select suitable materials of construction.

The process can be carried out in one or multiple batch reactors, possibly in fed-batch operation, and/or in a continuously operating system in one reactor or in a cascade of continuous flow reactors, optionally with multiple feeding points.

It was found that when adding at least about 0.6 molar equivalents of carbon oxide delivering agent on ethyleneamine compound, the yield of ethyleneamines increases considerably and also the amount of side products decreases.

Hence it is preferred to have the molar ratio of CO2 and/or carbon oxide delivering agent to ethyleneamine compound at least about 0.6 to 1.

Preferably, the molar amount of CO2 and/or carbon oxide delivering agents on ethyleneamine compounds is between about 0.7 and about 20 molar equivalents of carbon oxide delivering agent on moles of amine functional compound, and more preferably it is between about 0.7 and about 6:1, even more preferably between about 0.8:1 and about 3:1.

In another embodiment that leads to a high yield, the molar ratio of hydroxy-functional compound to ethyleneamine compound is at least about 0.7:1 and the molar ratio of carbon oxide delivering agent to ethyleneamine compound is at least about 0.05:1. In such embodiments the yield of ethyleneamines is also high.

Even more preferably the molar ratio of hydroxy-functional compound to ethyleneamine compound is between about 0.8 and about 5:1 and the molar ratio of carbon oxide delivering agent to amine functional compound is between about 0.2:1 and about 20:1.

Yet even more preferably the molar ratio of hydroxy-functional compound to ethyleneamine compound is between about 1:1 and about 2:1 and the molar ratio of carbon oxide delivering agent to ethyleneamine compound is between about 0.7:1 and about 3:1.

In one embodiment, to achieve a high selectivity of ethyleneamine on starting materials, especially on hydroxy-functional compound, the molar ratio of hydroxy-functional compound to ethyleneamine compound is preferably between about 0.05:1 and about 0.7:1 and the molar ratio of CO2 and/or carbon oxide delivering agent to ethyleneamine compound is higher than the molar ratio of hydroxy-functional compound to ethyleneamine compound.

More preferably the molar ratio of CO2 and/or carbon oxide delivering agent to ethyleneamine compound is at least about 10% higher than the molar ratio of hydroxy-functional compound to ethyleneamine compound. In another more preferred embodiment the molar ratio of hydroxy-functional compound to ethyleneamine compound is between about 0.1 and about 0.5.

It should be noted that carbon oxide delivering agents exist that contain more than one carbonyl group that can be released from the molecule for transfer to the hydroxy-functional compound, such as for example DU-TETA. When determining the molar ratio for such compounds there should be an adjustment for the molar amount of carbon oxide they can release for transfer to the hydroxyl-functional compound. Accordingly, about 1 mole of DU-TETA should be considered about 2 moles of carbon oxide delivering agent.

The molar ratio, as above, between compounds is determined by the reactants in the process, independent of the dosing regime used for the reactants.

Elimination Step

In the elimination step of the process as contemplated herein the CO2 adduct of polyethyleneamine compound is converted to the corresponding polyethyleneamine compound. It is called an elimination step because the carbonyl group is eliminated from the molecule.

There are various ways to carry out the elimination step.

In one embodiment, the elimination step comprises the step of reacting the CO2 adduct of polyethyleneamine compound with water to form CO2 and the corresponding ethyleneamine compound. This embodiment is also indicated herein as a desorption step.

In another embodiment the elimination step is carried out by reacting the CO2 adduct of polyethyleneamine compound with an inorganic base, resulting in the formation of a polyethyleneamine compound and a carbonate salt. This step is also indicated herein as a caustic treatment step. Within the context of the present disclosure, an inorganic base is a Lewis or Brosted base which does not contain carbon-carbon bonds. In many embodiments the inorganic base contains a metal, alkali metal or alkaline earth metal cation, and in many embodiments it is a Brønsted base. Preferably the inorganic base is a strong inorganic base which is a base that does not contain carbon-carbon bonds and has a pKb of less than about 1.

In another embodiment, the elimination step is carried out by transferring the carbonyl group from the CO2 adduct of the polyethyleneamine compound to a compound having a —NH—CH2-CH2-NH— moiety or a NH-CH2-CH2-OH moiety, or HO—CH2-CH2-OH. This step is also indicated as a CO2 transfer step.

In one embodiment of the present disclosure, the elimination step comprises a first elimination step and a further elimination step, wherein the first elimination step and the further elimination step are independently selected from the group of

a desorption step in which the CO2 adduct of polyethyleneamine compound is reacted with water to form CO2 and the corresponding polyethyleneamine compound,

a caustic treatment step in which CO2 adduct of polyethyleneamine compound is reacted with an inorganic base, resulting in the formation of a polyethyleneamine compound and a carbonate salt, and

a CO2 transfer step, wherein the carbonyl group from the CO2 adduct of the polyethyleneamine compound is transferred to a compound having a —NH—CH2-CH2-NH-moiety or a NH-CH2-CH2-OH moiety, or HO—CH2-CH2-OH,

wherein the first elimination step converts part of the CO2 adducts of polyethyleneamines present in the feed thereto into the polyethyleneamine compounds, while part of the CO2 adducts of polyethyleneamines present in the feed to the first elimination step is not converted in the first elimination step, and is provided to the second elimination step. Of course, provision of further elimination steps is also possible.

It may be preferred for the first elimination step to be a desorption step or a CO2 transfer step and the further elimination step to be a desorption step or a caustic treatment step, wherein the steps are not the same.

In one embodiment the elimination step comprises a desorption step in which not all CO2 adducts are converted to polyethyleneamine compounds. Thus, the product resulting from the desorption step may still comprise CO2 adducts of polyethyleneamine compounds. If this is the case, it has been found that the CO2 adducts are generally CO2 adducts of higher polyethyleneamine compounds rather than CO2 adducts of lower-boiling starting materials. In this case, if a separation step is carried out, it results in the separation of, in the first place, starting materials, in the second place, a product fraction of higher polyethyleneamine compounds and in the third place a fraction comprising CO2 adducts of higher polyethyleneamine compounds.

Desorption Step

In the desorption step carried out in one embodiment of the present disclosure, CO2 adducts of ethyleneamine compounds are converted into ethyleneamine compounds by reaction with water, with removal of CO2. The reaction takes place in the liquid phase.

The reaction with water generally takes place at a temperature of at least about 150° C. If the reaction temperature is below about 150° C., CO2 adducts of ethyleneamine compounds will not react to a significant extent. It is preferred for the reaction to be carried out at a temperature of at least about 180° C., in particular at least about 200° C., more in particular at least about 230° C., or even at least about 250° C. Preferably the temperature during this step does not exceed about 400° C., in particular at most about 350° C., more in particular at most about 320° C.

The pressure during the process is not critical, as long as the reaction medium is in the liquid phase. As a general range, a value of from about 0.5 to about 100 bara may be mentioned, depending on the desired temperature. It is preferred for the CO2 removal step to be carried out at a pressure of at least about 5 bar, in particular at least about 10 bar, to maintain a sufficient amount of amine and water in the medium. In view of the high costs associated with high-pressure apparatus, it may be preferred for the pressure to be at most about 50 bar, in particular at most about 40 bar.

The amount of water depends on the desired degree of conversion and on the process conditions. In general, the amount of water is at least about 0.1 mole water per mole CO2 adduct moiety in the feedstock. Higher amounts are often used, e.g., at least about 0.2 mole per mole CO2 adduct moiety, in particular at least about 0.5 mole water per mole CO2 adduct moiety. The maximum is not critical for the process as contemplated herein but too large amounts of water will lead to unnecessarily large equipment being required. As a general maximum an amount of at most 500 mole water per mole cyclic ethylene CO2 adduct moiety may be mentioned, in particular at most about 300 mole, more in particular at most about 200 mole, in some embodiments at most about 100 mole, or at most about 50 mole.

Depending on the reaction temperature and the desired degree of conversion, the reaction time can vary within wide ranges, e.g., at least one minute, in particular at least about 5 minutes, more in particular between about 15 minutes and about 24 hours. In one embodiment, the reaction time may be at least about 30 minutes, or at least about 1 hour. It may be preferred for the reaction time to vary between about 1 hour and about 12 hours, in particular between about 1 hour and about 6 hours. When using lower temperatures, longer reaction times may be required to obtain the desired degree of conversion.

In one embodiment of the present disclosure, the desorption step is carried out by reacting CO2 adducts of ethyleneamine compounds in the liquid phase with water in an amount of about 0.1-about 20 mole water per mole CO2 adduct moiety, at a temperature of at least about 230° C., with removal of CO2. It has been found that the use of a low amount of water in combination with a relatively high temperature and CO2 removal results in an efficient process which good conversion and low formation of side products. It has been found that it is possible in this embodiment of the process as contemplated herein to obtain good conversion with the relatively limited amount of water of at most about 20 mole water per mole CO2 adduct moiety. It has been found that it possible to work at even lower amounts of water, e.g., and amount of at most about 15 mole water per mole CO2 adduct moiety, more in particular an amount of at most about 10 mole water per mole CO2 adduct moiety, or even at most 5 mole water per mole CO2 adduct moiety.

The range of from about 0.1-about 20 mole water per mole CO2 adduct moiety refers to the entire amount of water added during the process, calculated on the amount of urea moieties in feedstock at the start of the reaction. To obtain full conversion, 1 mole of water is required per mole CO2 adduct moiety to be converted. As full conversion is not always necessary, lower amounts of water may be possible. Therefore, water is used in an amount of at least about 0.1 mole per mole CO2 adduct moiety. Higher amounts are often used, e.g., at least about 0.2 mole per mole CO2 adduct moiety, in particular at least about 0.5 mole water per mole CO2 adduct moiety.

Water can be added at the beginning of the desorption step in a single dosing. It is preferred, however, to add the water during the process, in several dosings or continuously. In a continuous operation multiple feedpoints may be used. By matching the amount of water added to the amount of water consumed by the reaction, the excess water in the reaction mixture can be limited. It has been found that this limits the formation of side products.

The molar ratio of water to urea moieties is calculated on the water present in the liquid reaction medium. If water is added in the form of steam, which may be an attractive embodiment to combine water addition with the provision of heat to the reaction mixture, the majority of water in the steam will not be absorbed in the liquid reaction medium. It is within the scope of the skilled person to regulate the conditions of a water addition process via stream in such a way that the desired amount of water is absorbed by the reaction medium. The water can also be present in the feedstock from the beginning of the reaction, e.g., as a result of the process by which the feedstock was produced. Water can also be added as a liquid.

In one embodiment of the desorption step, CO2 is removed. CO2 removal can be carried out when the conversion of the ethyleneureas into ethyleneamine compounds has been completed. However, it is preferred to carry out CO2 removal during the reaction. CO2 removal can be carried out in manners known in the art. The most basic way to do this it to vent the reaction vessel. A stripping fluid, in particular a stripping gas can be used to increase CO2 removal rate. Other measures to improve removal of CO2 will be evident to the skilled person, and include measures like stirring of the reaction mixture, sparging of stripping gas, thin-film evaporation, use of packing or trays, etc.

Where a stripping gas is used, the flow rate is typically at least about 1 m³ per about 1 m³ reactor volume per hour (at reaction temperature and pressure), and at most about 100 m³ per about 1 m³ reactor volume per hour (at reaction temperature and pressure). The stripping flow rate can be generated by evaporation of a liquid inside the reactor vessel, resulting in in situ generation of stripping gas. The ranges above also apply to this embodiment. Of course, it is also possible to combine the addition of stripping gas with the in situ formation of stripping gas.

The CO2-containing stripping fluid removed from the CO2 removal step can, for example, comprise from about 1 to about 99 mol. % CO2. In other embodiments, the stripping fluid may comprise from about 1-about 80 mol. % CO2, or about 1-about 60 mol. % CO2. In some embodiments, the effluent from the CO2 removal step may comprise from about 1-4 about 0 mol. % CO2, or about 1-about 20 mol. % CO2. Lower CO2 contents make for more efficient stripping, but also for the use of more stripping gas. It is within the scope of the skilled person to find an appropriate balance between these parameters.

If so desired the desorption step can be carried out with water in the presence of an amine compound selected from the group of primary amines, cyclic secondary amines, and bicyclic tertiary amines.

Primary amines are amine functional compounds in which the amine group is of the formula R4-NH2 and wherein R4 can be any organic group, preferably an aliphatic hydrocarbon with optional heteroatoms such as oxygen and/or nitrogen. Secondary cyclic amines are amines of the formula R5-NH—R6, wherein R5 and R6 together form a hydrocarbon ring, optionally with heteroatoms such as oxygen and/or nitrogen, preferably a piperazine ring. Tertiary bicyclic amines are amines of the formula R7-N(—R9)-R8 where R7 and R8 together form a hydrocarbon ring—optionally with heteroatoms such as oxygen and/or nitrogen—and R7 and R9 together form another hydrocarbon ring—optionally with heteroatoms such as oxygen and/or nitrogen. On all the above groups R4 to R9 substituents can be present, like alkyl or hydroxyalkyl groups. Primary amines, cyclic secondary amine and bicyclic tertiary amines all contain a sterically relatively unhindered amine group. In this document a compound is defined as a primary amine or a secondary cyclic amine or a tertiary bicyclic amine if one of the amine groups in the compound is a primary amine or secondary cyclic amine or a tertiary bicyclic amine group, independent of if this compound contains further amine groups that may be different in their nature. A compound can also contain two or more different amine functionalities, e.g. a primary amine and a secondary cyclic amine functionality or a primary amine, a secondary cyclic amine and a tertiary bicyclic amine functionality.

Preferred examples of primary amines are alkylamines, linear ethyleneamines, and alkanolamines Preferred examples of cyclic secondary amines are amines that contain a terminal piperazine ring. Preferred examples of bicylic tertiary amines are 1,4-diazabicyclo[2.2.2]octane (DABCO), 1,4-diazabicyclo[2.2.2]octan-2-yl)methanol and 1-azabicyclo[2.2.2]octane (Quinuclidine).

The amine compound is preferably a compound with more than one amine group wherein at least one of the amine groups is a primary amine, even more preferably it is an amine wherein two amine groups are a primary amine

Preferred amine compounds include ethylenediamine (EDA), N-methylethylenediamine (MeEDA), diethylenetriamine (DETA), ethanolamine (MEA), aminoethylethanolamine (AEEA), piperazine (PIP), N-aminoethylpiperazine (AEP), 1,4-diazabicyclo[2.2.2]octane (DABCO), 1,4-diazabicyclo[2.2.2]octan-2-yl)methanol, triethylenetetramine (TETA), N-diethyldiamine-2-imidazolidinone (U1TETA), N, N′-diaminoethylpiperazine (DAEP), N, N′-diaminoethyl-2-imidazolidinone (U2TETA), tetraethylenepentamine (TEPA), pentaethylenehexamine (PEHA), and the mono cyclic ureas of TEPA and PEHA (i.e. U1TEPA, U2TEPA, U1PEHA, U2PEHA, U3PEHA) and the dicyclic urea isomers of PEHA (i.e. DUPEHA), a polyethyleneimine (PEI) or an ethyleneamine on a solid carrier.

The amine compound is preferably present in a molar amount of between about 0.001 and about 100 equivalents per mole CO2 adduct moiety, more preferably between about 0.01 and about 50 equivalents, even more preferably between about 0.05 and about 30 equivalents, yet more preferably between about 0.15 and about 25 equivalent and most preferably between about 0.20 and about 20 equivalents.

In the desorption step, CO2 adducts of ethyleneamine compounds are converted to CO2 and ethyleneamine compounds. It is preferred for at least about 10 mole % of the CO2 adduct moieties in the system to be converted to the corresponding ethyleneamine moieties. The maximum will depend on the following desorption and recycle steps.

Treatment with (Strong) Inorganic Base

In one embodiment, an elimination step is carried out using a (strong) inorganic base. Within the context of the present disclosure, a strong inorganic base is a base with a material which does not contain carbon-carbon bonds and which has a pKb of less than about 1.

In one embodiment, the strong inorganic base is selected from the group of metal hydroxides, in particular from the group of hydroxides of alkaline and earth alkaline metals, in particular from sodium hydroxide, potassium hydroxide, lithium hydroxide, calcium hydroxide, magnesium hydroxide, and barium hydroxide. In one embodiment, the strong inorganic base is selected from the group of metal oxides, in particular from the group of oxides of alkaline and earth alkaline metals, in particular from calcium oxide, magnesium oxide, and barium oxide. Selecting a strong inorganic base from the group of sodium hydroxide, potassium hydroxide, magnesium (hydr)oxide, and calcium (hydr)oxide may be preferred. The use of sodium hydroxide and potassium hydroxide may be particularly considered preferred. Other strong inorganic bases may also be used, such as ammonium hydroxide. As will be evident to the skilled person, mixtures of various inorganic bases can be used. Compounds comprising a base in addition to other components can also be used, as can be compounds which will be converted into inorganic bases in the reaction medium.

The lower limit of the molar ratio of inorganic base to CO2 adduct moieties is not critical. A value of at least about 0.2:1 may be mentioned. If it is desired to obtain full conversion of the CO2 adduct moieties into the corresponding ethyleneamine compound, the use of larger amounts may be preferred, e.g., in a molar ratio of at least about 0.5:1, in particular at least about 1:1. It may be preferred to use larger amounts to increase the reaction rate, e.g., a molar ratio of inorganic base to CO2 adduct moiety of at least about 1.5:1, in particular at least about 2:1.

As large amounts of base do not contribute to further conversion but will lead to additional costs, it is preferred for the molar ratio of the inorganic base to the molar amount of CO2 adduct moieties in the product provided to the treatment with the inorganic base to be at most about 20:1, in particular at most about 15:1, more in particular at most about 10:1. It has been found that even lower amounts of inorganic base can suffice, in contrast to what has been disclosed in the prior art. More in particular, it has been found that good results can be obtained at a molar ratio of inorganic base to CO2 adduct moieties of at most about 7.5:1, in particular at most about 6.5:1, even more in particular at most about 5.5:1. It has been found that the use of a molar ratio of at most about 5.5:1 results in full conversion of the CO2 adduct moieties and high yield of the resulting ethyleneamine compounds. It may be preferred to use even less inorganic base per mole of CO2 adduct moiety, e.g., in a more ratio of at most about 5:1, in particular at most about 4:1, more in particular at most about 3:1. The molar ratio is calculated on the molar amount of CO2 adduct moieties in the feed provided to the caustic treatment step.

The treatment with inorganic base can, for example, be carried out by contacting the material to be treated with a concentrated aqueous solution of the inorganic base. Depending on the nature of the base and the further composition of the reaction mixture, it may also be possible to add the base in solid form and dissolve it in the reaction medium. As will be clear to the skilled person, the aim is to bring the base in a dissolved state, so that the hydroxy groups can react with the CO2 adduct, while avoiding unnecessary dilution of the reaction medium.

The reaction can be carried out at a temperature between room temperature and about 400° C. The temperature and pressure should be selected such that the reaction mixture is in the liquid phase. Higher temperatures are advantageous because they lead to decreased reaction times. It may be preferred to carry out the reaction at a temperature of at least about 100° C., in particular at least about 140° C., in particular at least about 170° C. On the other hand, higher temperatures may lead to the undesired formation of side products. It may therefore be preferred to carry out the reaction at a temperature of at most about 350° C., in particular at most about 280° C.

Depending on the reaction temperature, the reaction time can vary within wide ranges, e.g., between about 15 minutes and about 24 hours. It may be preferred for the reaction time to vary between about 1 hour and about 12 hours, in particular between about 1 hour and about 6 hours. When using lower amounts of base, longer reaction times may be required to obtain the desired degree of conversion.

In one embodiment, as discussed elsewhere herein, the caustic treatment step from the second reaction sequence may be combined with a caustic treatment elimination step from the first reaction sequence. In that case, as the conversion of the CO2 adduct of the ethyleneamine compound into the corresponding ethyleneamine compound, requires more stringent conditions than the conversion of the ethyleneamine hydrohalide salt into ethyleneamine Therefore, if the two reactions are to be combined in a single step, the conditions and the amount of base should be selected such that both reactions take place. The conditions described above for the conversion of the CO2 adduct of the ethyleneamine into the corresponding ethyleneamine should suffice.

Upon completion of the reaction, a reaction mixture will be obtained which contains ethyleneamine compounds and a carbonate salt of the inorganic base. The salt can be removed by methods known in the art, e.g., by filtration where the salt is in solid form. The process as contemplated herein can be carried out in batch operation, fed-batch operation, or in a continuous operation, e.g., in a cascade of continuous flow reactor. Depending on the scale of the operation, continuous operation may be preferred.

Combination of Elimination Steps

A particular combination of elimination steps include a desorption step followed by a treatment with strong inorganic base, optionally after a separation step in which desired compounds have been removed.

In one embodiment, this combination encompasses the conversion of cyclic ethyleneureas into their corresponding ethyleneamines by a process comprising

in a first step converting cyclic ethyleneureas into their corresponding ethyleneamines by reacting cyclic ethyleneureas in the liquid phase with water with removal of CO2, so as to convert between about 5 mole % and about 95 mole % of ethyleneurea moieties in the feedstock to the corresponding amines, and

in a second step adding a inorganic base and reacting cyclic ethylene ureas remaining from the first step with the inorganic base to convert them completely or partially into their corresponding ethyleneamines

Another particular combination of elimination steps include a combination of one or more desorption steps with one or more reactive separation steps. The reactive separation encompasses CO2 transfer wherein the carbonyl group from the CO2 adduct of the product polyethyleneamine compound is transferred to a compound having a —NH-CH2-CH2-NH— moiety or a NH-CH2-CH2-OH moiety, or HO—CH2-CH2-OH.

In one embodiment this combination encompasses the conversion of a feedstock comprising cyclic ethyleneureas into their corresponding ethyleneamines, by a process comprising

a desorption step in which cyclic ethyleneureas are converted into their corresponding ethyleneamines by reacting cyclic ethyleneureas in the liquid phase with water with removal of CO2,

a reactive separation step wherein cyclic ethyleneureas are converted into their corresponding ethyleneamines by reaction with an amine compound selected from the group of primary amines or secondary amines which have a higher boiling point than the ethyleneamines formed during the process.

The reactive separation step may preferably be carried out as a reactive distillation step. This embodiment is also discussed above in the context of the reaction step.

In one embodiment the desorption step precedes the reactive separation step. In another embodiment, the reactive separation step precedes the desorption step. It is also possible to perform at least two desorption steps, with one or more reactive separation step being performed in between, or at least two reactive separation steps, with one or more reactive desorption steps being performed inbetween.

The reactive separation step may be conducted at any suitable pressure. During the reaction, the pressure in the reactive separation system preferably is at most about 127 bara, more preferably at most about 50 bara, and even more preferably at most about 25 bara. Depending on the composition of the reaction medium, lower pressures may be applied, e.g., less than about 15 bar, or less than about 5 bar. The process can also be carried out at a pressure below atmospheric pressure, such as less than about 700 mbara, more preferably below about 100 mbara, even more preferably below about 25 mbara, and most preferably below about 5 mbara. In general the pressure will be at least about 0.1 mbara.

The reactive separation step is preferably carried out at a temperature of at least about 150° C., in particular at least about 180° C., in some embodiments at least about 200° C., or at least about 230° C., sometimes at least about 250° C. Preferably the temperature during the process does not exceed about 400° C., more preferably about 350° C. In one embodiment, the reactive separation step amine removal step is carried out at a temperature in the range of from about 180-about 300° C. and a pressure of at most about 2000 mbara, in particular at most about 1000 mbara, more in particular at most about 500 mbara, more in particular at most about 200 mbara. It may be preferred to carry out the reactive separation step at a temperature of from about 200-about 260° C. and a pressure of at most about 50 mbara. The reactive separation step generally is performed for a time of between about 1 minute and about 12 hours. Preferably the reactive separation step is run in less than about 10 hours, more preferably in less than about 8 hours, most preferably less than about 5 hours.

In some embodiments it is favorable to at least partially combine the reaction step with the separation, and/or elimination step by performing a reactive separation step, such as a reactive distillation. In a reactive separation step the above reaction step finds place under conditions selected such that the CO2 adduct of the starting compounds reacts to give CO2 adduct of product polyethyleneamine and in the same reactive separation the formed CO2 adduct of product polyethyleneamine is either separated from other components, or transfers it CO moiety to another component in the reactor, which can be either remaining starting compounds or byproducts.

In one embodiment CO2 adducts of ethyleneamine compounds are converted into their corresponding ethyleneamine compounds by reaction with an amine compound chosen from the group of primary amines or secondary amines that have a higher boiling point than the ethyleneamine compounds formed during the process, wherein the process is a reactive separation process and the reaction mixture contains less than about 10 wt % of water on the basis of total weight of the reaction mixture. It may be preferred to carry out the reaction in less than about 7 wt % of water on total reaction mixture. It may be preferred for the pressure to be less than about 25 bara, in particular less than about 500 mbara. In general, the reaction will be done at a temperature of at least about 150° C.

The second reaction sequence

The second reaction sequence comprises the steps of

in a ethylenedichloride reaction step reacting ethylenedichloride with at least one compound selected from the group of ammonia, ethyleneamine and/or ethanolamine to form a hydrochloride salt of ethyleneamine and/or ethanolamine,

in a caustic treatment step reacting the hydrochloride salt of ethyleneamine or ethanolamine with a base to form ethyleneamine compound and an inorganic chloride salt,

in a salt separation step separating the inorganic salt from the ethyleneamine compound.

The ethylenedichloride reaction step is generally carried out in the range of from about 100-about 220° C., in particular in the range of from about 120-about 200° C.

The pressure in the ethylenedichloride reaction step is generally in the range of from about 1-about 80 bar, in particular from about 5-about 80 bar. Especially in the case where ammonia is used as reactant, it may be preferred to operate at relatively high pressures, e.g., in the range of from about 10-about 80 bar, in particular from about 20-about 50 bar.

The time necessary for the reaction will depend on the desired degree of conversion, the nature and concentration of the reactants, and the reaction temperature. In general, the reaction time will be between about 5 minutes and about 24 hours, more specifically in the range of about 10 minutes to about 12 hours, in some embodiments in the range of about 0.5 to about 8 hours.

In a caustic treatment step the hydrochloride salt of ethyleneamine or ethanolamine formed in the ethylenedichloride reaction step is reacted with a base to form ethyleneamine compound and an inorganic chloride salt, with a chloride salt as side product.

The use of strong inorganic bases such as NaOH and KOH is generally preferred from an economic point of view, and because the resulting Na-halide and K-halide salts are relatively easy to separate from the product.

The amount of base can be calculated from the amount of hydrochloride salt of ethyleneamine or ethanolamine. In general, the molar ratio of hydroxide ions derived from the base to chloride-ions in the salt is in the range of from about 1:1 to about 10:1. The base can be provided in dissolved form, e.g., in the form of a solution in water. the reaction will generally take place at a temperature in the range of from about 0 to about 200° C. in particular in the range of from about 10 to about 150° C. Reaction pressure is not critical and can. e.g., be in the range of atmospheric to about 15 bar, more in particular in the range of atmospheric to about 3 bar. In general, the neutralization step treatment time will be between about 1 minute and about 24 hours, more specifically in the range of about 10 minutes to about 12 hours, in some embodiments in the range of from about 0.5 to about 8 hours.

The second reaction sequence also comprises a salt separation step in which the inorganic chloride salt is separated from the ethyleneamine compound. This step can be carried out in various manners. For example, the ethyleneamine compound can be removed by evaporation. For another example, the ethyleneamine compound can be removed by crystallization followed by phase separation. For a further example, the addition of an anti-solvent may result in precipitation of the ethyleneamine compound, while keeping the halide salt in solution, or vice versa, followed by removal of the precipitate. Combinations of the various separation methods are also possible.

Connection of the First and Second Reaction Sequences

In the process as contemplated herein, the first reaction sequence and the second reaction sequence are connected in that at least one of the following takes place:

effluent from a step in the first reaction sequence is provided as starting material to a step in the second reaction sequence,

effluent from a step in the second reaction sequence is provided as starting material to a step in the first reaction sequence,

a step from the first reaction sequence and a step from the second reaction sequence are combined, or

effluent from a step in the first reaction sequence is combined with effluent from a step in the second reaction sequence.

There are numerous ways in which the first reaction sequence and the second reaction sequence can be connected.

In one embodiment an ethyleneamine produced in the second reaction sequence is provided to one or more of the absorption step, the chain extension step, and the elimination step in the first reaction sequence, in particular to the chain extension step and/or to the elimination step. This embodiment is advantageous because it allows an increase in product slate flexibility by shifting the output of products which are less in demand to those which are in higher demand. Further, by transferring unseparated (reaction) mixtures the load on the separation step may be reduced which increases process efficiency in terms of operational cost (energy, steam) and capacity.

In one embodiment a CO2 adduct of a ethyleneamine compound from the first reaction sequence is provided to the caustic treatment step in the second reaction sequence. This allows the elimination step from the first reaction sequence and the caustic treatment from the second reaction sequence to be combined, making for improved use of apparatus. The work-up of the resulting product is also combined, again making for more efficient use of apparatus and saving on CAPEX and OPEX.

In one embodiment the elimination step in the first reaction sequence comprises a caustic treatment, and product of the caustic treatment in the first reaction sequence is combined with product from the caustic treatment in the second reaction sequence, and the combined product is subjected to the salt separation step. This embodiment is close to the embodiment discussed above. Here, the product-workup is combined but the elimination step and the caustic treatment step are carried out separately, and can thus be tailored to the specified conditions. For example, the caustic treatment in the first reaction sequence and the caustic treatment in the second reaction sequence may yield different salts, and performing the caustic treatments separately may make it easier to process the resulting salts steams.

In one embodiment an ethyleneamine reaction mixture from the first reaction sequence is combined with an ethyleneamine reaction mixture from the second reaction sequence, and the combined product is subjected to a separation step. Various ways of combining the separation steps may be envisaged, ranging from combining the entire product of both reaction sequences. combining the entirety of the product of one reaction sequence with part of the product of the other reaction sequence, and combining part of the product of one reaction sequence with part of the product from another reaction sequence. In general, combining separation steps makes for increased efficiency from an operating point of view, both as regards to apparatus costs and as regards to operating costs.

In one embodiment a CO2 adduct of an ethyleneamine from the first reaction sequence is provided to the ethylenedichloride reaction step from the second reaction sequence.

An advantage of this embodiment is that it may increase product slate flexibility by shifting the output of products which are less in demand to those which are in higher demand, including CO2 adducts of ethyleneamine compounds as products. A particular advantage of this embodiment is that the provision of CO2 adducts of ethyleneamine compounds to the second reaction sequence may ensure a higher yield of straight-chain higher ethylene amine product compounds, as the urea group may act as blocking group, therewith reducing the formation of cyclic compounds.

In one embodiment a CO2 adduct formed in the first reaction sequence is provided to the ethylenedichloride reaction step in the second reaction sequence, and a CO2 adduct from the ethylenedichloride reaction step or the caustic treatment step in the second reaction sequence is provided to the elimination step in the first reaction sequence. This embodiment combines the advantages of the previous embodiment with an efficient manner of converting the carbonyl-containing reaction product into the corresponding ethyleneamine compound.

In one embodiment the first reaction sequence and the second reaction sequence are connected in that:

ethyleneamine produced in the second reaction sequence is provided to one or more positions of the absorption step, the chain extension step, and the elimination step in the first reaction sequence, in particular to the chain extension step and/or to the elimination step and

ethyleneamine product from the salt separation step in the second reaction sequence is provided to a fractionation step, where it is fractionated into different ethyleneamine product fractions, and an ethyleneamine compound fraction is withdrawn from the elimination step in the first reaction sequence and provided to said fractionation step from the second reaction sequence and/or a product withdrawn from a separation step in the first reaction sequence is provided to the fractionation step in the second reaction sequence.

This combination of providing one or more fractions from the fractionation step in the second reaction sequence to the first reaction sequence and vice versa allows a particularly efficient use of equipment, and makes it possible to tailor the nature of the products produced to the market demand

The figures of the present application show various manners in which this can be effected. It will be evident to the skilled person that various manners of connecting the sequences can be combined, even if they are provided in different figures.

The present disclosure will be elucidated with reference to the figures, without being limited thereto or thereby. For all processes and figures present herein the following applies.

Intermediate separation steps may be present, also if they are not specified or shown.

Effluents from process steps can be provided to other process steps in part or in their entirety, whether or not after a separation step has been carried out.

Appropriate recycle of starting materials or intermediate products may be carried out, also if it is not specified or shown.

Purge streams and make-up streams may be present, also if they are not specified or shown.

Reactants may be provided individually or in combination, also if this is not specified or shown.

The different steps in the Figures do not necessarily refer to different units or reactors.

Embodiments of the present disclosure may be combined, unless they are mutually exclusive.

Elements of the figures can be combined, and as will be evident from the description, not all elements shown are essential to a specific embodiment.

Sometimes reaction streams are indicated with the shorthand wording ethyleneamine compound. This wording should not be interpreted as limiting on the content of the fraction, which, as will be evident to the skilled person, may contain other compounds also, e.g., if present, ethanolamine compounds, or, if present, CO adducts of ethyleneamine or ethanolamine compounds.

FIG. 1 illustrates a first embodiment of the present disclosure, in which the two reaction sequences are connected in that effluent from a step in the second reaction sequence is provided to a step in the first reaction sequence.

In FIG. 1, a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH is provided through line 1 to adduction step 2 where a carbon oxide delivering agent is added through line 3. The resultant adduct is provided to a chain-extension reaction step 5 through line 4. Additional reactants can be provided to chain-extension reaction step 5 through lines not shown. For example, if the product from the adduction step is an CO2 adduct of an ethyleneamine compound, an ethanolamine compound can be provided to chain-extension reaction step 5. The effluent from the chain-extension reaction step 5 is provided to elimination step 7 through line 6. In the CO2 elimination step 7, CO2 adduct of ethyleneamine compound is converted to the corresponding ethyleneamine compound, which is withdrawn through line 9. The compound comprising the carbonyl group, eliminated from the CO2 adduct of the product ethyleneamine compound is withdrawn through line 10. This part of the figure thus illustrates the first reaction sequence.

In the other part of the figure, ethylenedichloride is provided through line 301 to EDC reaction 300, where it is combined with at least compound selected from the group of ammonia, ethyleneamine and/or ethanolamine provided through line 302. A reaction medium comprising a hydrochloride salt of ethyleneamine compound is withdrawn through line 303, and provided to a caustic treatment step 320. In caustic treatment step 320 the hydrochloride salt of ethyleneamine compound is reacted with a strong inorganic base, provided through line 321 to form ethyleneamine compound and an inorganic chloride salt. The inorganic chloride salt is separated from the ethyleneamine compound in a salt separation step (not shown), and is withdrawn through line 322. The ethyleneamine compound fraction is withdrawn through line 324, and, in the case illustrated in this figure, provided to a fractionation step 330, where the ethyleneamine compound fraction is separated into different fractions. In the embodiment illustrated in FIG. 1 the two process sequences are connected in that an ethyleneamine compound fraction is withdrawn from separation step 330 from the second reaction sequence and provided to the first reaction sequence, in this case to the adduction step 2 through line 401. As will be clear to the skilled person, the composition and amount of the fraction may be selected at will. Optionally, intermediate separation steps may be carried out. If so desired, a further fraction can be withdrawn from separation step 330 and provided to chain-extension reaction step 5 through line 402. The composition of the two fractions may be the same or different, and it will be clear to the skilled person that it is also possible to have only one of fractions 401 and 402. A further ethyleneamine compound fraction is withdrawn through line 331.

Thus, in one embodiment as contemplated herein an ethyleneamine produced in the second reaction sequence is provided to the absorption step and/or the chain extension step in the first reaction sequence.

This embodiment may be attractive because it allows the use of low-molecular weight ethyleneamine compound fractions generated in the second reaction sequence to be used as starting material in the manufacture of higher molecular weight ethyleneamine compounds through the process of the first reaction sequence. In general, this embodiment allows an increase in product slate flexibility by shifting the output of products which are less in demand to those which are in higher demand. Further, by transferring unseparated (reaction) mixtures the load on separation unit 330 is reduced which increases process efficiency in terms of operational cost (energy, steam) and capacity.

FIG. 2 illustrates a second embodiment of the present disclosure, in which the two reaction sequences are connected in that effluent from a step in the first reaction sequence is provided to a step in the second reaction sequence.

FIG. 2 shows the same entities as FIG. 1. However, instead of lines 401 and 402 present in FIG. 1, in FIG. 2 an ethyleneamine compound fraction is withdrawn from elimination step 7, through line 403 and provided to fractionation step 330. While not essential to the present disclosure, FIG. 2 also contains a separation step 14, which is provided after the elimination step 7. The separation step 14 results in the separation of different fractions. For example, starting materials and/or intermediate compounds can be withdrawn through line 16. They can be provided to adduction step 2 and/or chain-extension reaction step 5 through lines not shown. The separation step 14 also yields a product fraction of higher ethyleneamine compounds which is withdrawn through line 15. A fraction from separation step 14 from the first reaction sequence can be provided to fractionation step 330 from the second reaction sequence, e.g., as illustrated, through line 404.

Thus, in one embodiment as contemplated herein, ethyleneamine product from the salt separation step in the second reaction sequence is provided to a fractionation step, where it is fractionated into different ethyleneamine product fractions, and an ethyleneamine compound fraction is withdrawn from the elimination step in the first reaction sequence and provided to said fractionation step from the second reaction sequence and/or a product withdrawn from a separation step in the first reaction sequence is provided to the fractionation step in the second reaction sequence.

This embodiment allows efficient and cost-effective tailoring of the separation steps. More specifically, process efficiency is increased by combining the separation units of both reaction sequences. This allows creating optimum capacity at minimum costs. By avoiding duplicate columns, redundancy is reduced. Further, in this embodiment the flexibility of the use of the separation units is increased, allowing tailored processing of the various fractions.

In a variation of this embodiment, the effluent from the salt separation step can be provided in its entirety to the separation section of the first reaction sequence.

FIG. 2A illustrates a preferred embodiment of the present disclosure, in which all of lines 401, 402, 403, and 404 are presented. This figure thus is an illustration of an embodiment of the present disclosure in which with the first reaction sequence and the second reaction sequence are connected in that:

ethyleneamine produced in the second reaction sequence is provided to the absorption step and/or the chain extension step in the first reaction sequence, and

ethyleneamine product from the salt separation step in the second reaction sequence is provided to a fractionation step, where it is fractionated into different ethyleneamine product fractions, and an ethyleneamine compound fraction is withdrawn from the elimination step in the first reaction sequence and provided to said fractionation step from the second reaction sequence and/or a product withdrawn from a separation step in the first reaction sequence is provided to the fractionation step in the second reaction sequence.

This combination of providing one or more fractions from the fractionation step in the second reaction sequence to the first reaction sequence and vice versa allows a particularly efficient use of equipment, and makes it possible to tailor the nature of the products produced to the market demand. It is possible to have either or both of streams as illustrated by 401 and 402 and either or both of streams as illustrated by 403 and 404.

FIG. 3 illustrates a further embodiment of the present disclosure. In the embodiment of FIG. 3 effluent from a step in the first reaction sequence is combined with effluent from a step in the second reaction sequence.

In FIG. 3 effluent comprising ethyleneamine compound withdrawn through line 9 from the elimination step 7 of the first reaction sequence is combined in separation section 501 with effluent withdrawn through line 324 from the caustic treatment step 320 after separation from the inorganic chloride salt. In this embodiment, the ethyleneamine compound produced by the first reaction sequence and the second reaction sequence is combined, and subjected to a combined separation section 501. Separation section 501 can comprise multiple separation steps, in particular distillation steps, carried out in multiple units. Of course, intermediate separation steps or fractionation steps, for example the removal of low-boiling starting materials, can be carried out between, respectively, elimination step 7 and separation section 501 and between caustic treatment 320 and separation section 501. Separation section 501 results in the formation of at least two effluent streams of different composition. FIG. 3 shows three effluent streams, namely stream 502, 503, and 504, but fewer or more effluent streams may also be used. Where separation section 501 comprises multiple units, each individual unit may generate one or more streams which can be regarded as effluent streams from the separation section. One of these streams, for example, is a lighter-boiling ethyleneamine fraction comprising, e.g. starting materials and low-boiling products, such as ethyeneamine and ethanolamine. This steam, or a part thereof, can, if so desired be recycled to earlier steps in the process, e.g., to adduction step 2, chain-extension reaction step 5, or EDC reaction 300 through lines not shown. A further of streams 502, 503, and 504 may be a high-boiling fraction, comprising for example, CO2 adducts of high-boiling ethyleneamines. This steam, or a part thereof, can be subjected to a caustic treatment, e.g. by providing it to caustic treatment step 320. It may, however, be preferred to subject it to a separate caustic treatment step. This is indicated in FIG. 3 for stream 504, which is provided to a caustic treatment step 505, where strong inorganic base is added through line 506, resulting in the formation of an ethyleneamine compound fraction withdrawn through line 507 and a carbonate salt withdrawn through line 508.

The use of a combined separation section as is illustrated in this embodiment enables more efficient use of separation equipment, and efficient tailoring of product fractions depending on prevailing market conditions. Reference is made to the advantages on linking separation units as provided above in the discussion of FIGS. 1, 2, and 2A.

FIG. 4 illustrates a further embodiment of the present disclosure. In the embodiment of FIG. 4, a step of the first reaction sequence and a step from the second reaction sequence are combined. More in particular, the first reaction sequence comprises an elimination step, in which CO2 adduct of product ethyleneamine compound is converted to the corresponding product ethyleneamine compound. This step can be carried out by reacting the CO2 adduct of the product ethyleneamine compound with a strong inorganic base, resulting in the formation of an ethyleneamine compound and a carbonate salt. This step can be combined with the caustic treatment step from the second reaction sequence, where the hydrochloride salt of ethyleneamine or ethanolamine compound is reacted with a base to form ethyleneamine compound and an inorganic chloride salt. In FIG. 4, this is illustrated by providing the effluent from the chain-extension reaction step 5 through line 6 to a separation step 509, where CO2 adduct of ethyleneamine compound is separated from the reaction medium and provided through line 510 to caustic treatment 320. Separation step 509 also generates a further effluent stream comprising, e.g., starting materials and ethyleneamine compounds, which is withdrawn through line 511. While it is possible to dispense with separation step 509 and provide the effluent of chain-extension reaction step 5 directly to caustic treatment 320, the use of an intermediate separation step is generally considered preferred, as it limits the volume of the reactant stream to the caustic treatment step. This embodiment makes for an efficient use of apparatus and combined separation and product workup. This combination of separation and product work-up results in improved CAPEX and OPEX as compared to the use of two separate separation and workup streams

In a variation of this embodiment, in the first reaction sequence a treatment with inorganic base is carried out, and the resulting mixture of inorganic salt and ethyleneamines is combined with the salt separation step in the second reaction sequence. In this case, both in the first reaction sequence and in the second reaction sequence a treatment with inorganic base is carried out, and the salt separation and further product workup are combined. This embodiment may be attractive because it allows carrying out the base treatments in the different reaction sequences under tailored conditions, while saving on apparatus by combining separation and product work-up. more specifically, having separate caustic treatment steps for compounds being in the form of a CO2 adduct and hydrochlorides will mean that conditions can be tailored to the compounds to be treated. The same applies to the salt separation step.

Thus, in one embodiment, CO2 adduct of a ethyleneamine compound from the first reaction sequence is provided to the caustic treatment step in the second reaction sequence, directly or after having passed a separation step. It may be attractive to combine this embodiment with the provision of ethyleneamine produced in the second reaction sequence to the absorption step and/or the chain extension step in the first reaction sequence, as described above in the context of FIG. 1.

Another embodiment of the present disclosure is the embodiment wherein a CO2 adduct of a ethyleneamine compound is provided to the ethylenedichloride reaction step. This may be advantageous to tailor the composition of the reaction product or to increase product slate flexibility by shifting the output of products which are less in demand to those which are in higher demand, including CO2 adduct compounds as products. A particular advantage of this embodiment is that the provision of CO2 adducts of ethyleneamine compounds to the second reaction sequence may ensure a higher yield of straight-chain higher ethylene amine product compounds, as the urea group may act as blocking group, therewith reducing the formation of cyclic compounds. FIG. 5 illustrates various embodiments of such a process.

In FIG. 5, line 405 allows the provision of CO2 adduct produced in adduction step 2 to be provided to EDC reaction step 300. Line 406 allows the provision of CO2 adduct produced in chain-extension reaction step 5 to be provided to EDC reaction step 300. It will be clear that it is not necessary to have both lines 405 and 406, although it is definitely possible. Whether it is desired to provide adduct withdrawn from the adduction step 2, from chain-extension reaction step 5, or from both, to the EDC reaction step 300 will depend on the product aimed for, where the provision of adduct from the chain-extension reaction step 5 will generally lead to higher-molecular weight product than the provision of product from the adduction step 2. It is possible, and may be preferred, to carry out an intermediate separation step (not shown) on the effluent from the adduction step 2 or chain-extension reaction step 5 before providing it to the EDC reaction 300. In this embodiment it may be desirable to provide CO2 adduct remaining after the caustic treatment 320 to elimination step 7, generally after the effluent from caustic treatment step 320 has been provided to a separation step. This may be attractive when the conditions in the caustic treatment step 320 are such that not all CO2 adduct will be converted to the corresponding amine in the caustic treatment step. Additionally or alternatively, it is also possible to provide ethyleneamine product from the elimination step, or from a separation step following the elimination step to the EDC reaction.

FIG. 6 shows an embodiment of the process as contemplated herein the effluent from the chain-extension reaction step 5 is provided through line 6 to a separation step 512, where CO2 adduct of ethyleneamine compound is separated from the reaction medium and provided through line 407 to EDC reaction 300. Separation step 512 also generates a further effluent comprising, e.g., starting materials and ethyleneamine compounds, which is withdrawn through line 513. While it is possible to dispense with separation step 512 and provide the effluent of chain-extension reaction step 5 directly to EDC reaction 300, the use of an intermediate separation step is generally considered preferred, as it limits the volume of the reactant stream to the caustic treatment step. In this embodiment elimination step 7 is thus combined with caustic treatment 320, which is attractive as it results in a reduced CAPEX and OPEX of the operation.

REFERENCE LIST

-   1 starting compound comprising a —NH—CH2-CH2-NH— moiety or a     —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH -   2 adduction step -   3 carbon oxide delivering agent, e.g., CO2 -   4 effluent from adduction step -   5 chain extension reaction step -   6 effluent from chain extension reaction step -   7 elimination step -   9 ethyleneamine compound -   10 compound comprising carbonyl group -   14 separation step -   15 ethyleneamine compound product fraction -   16 starting materials and/or intermediate products -   300 EDC reaction -   301 EDC -   302 compound selected from the group of ammonia, ethyleneamine     and/or ethanolamineammonia -   303 hydrochloride salt of ethyleneamine compound -   320 caustic treatment -   321 strong inorganic base -   322 chloride salt -   324 ethyleneamine compound -   330 fractionation step -   331 ethyleneamine compound -   401 ethyleneamine compound to adduction step -   402 ethyleneamine compound to chain extension reaction step -   403 ethyleneamine compound from elimination step to fractionation     step -   404 ethyleneamine compound from separation step to fractionation     step -   405 CO2 adduct of starting compound comprising a —NH—CH2-CH2-NH—     moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH -   406 CO2 adduct of starting compound comprising a —NH—CH2-CH2-NH—     moiety or a —NH—CH2-CH2-0H moiety, or HO—CH2-CH2-OH -   407 CO2 adduct of starting compound comprising a —NH—CH2-CH2-NH—     moiety or a —NH—CH2-CH2-0H moiety, or HO—CH2-CH2-OH -   501 separation section -   502 effluent stream -   503 effluent stream -   504 effluent stream -   505 caustic treatment -   506 strong inorganic base -   507 ethyleneamine compound -   508 carbonate salt -   509 separation step -   510 CO2 adduct of ethyleneamine compound -   511 effluent stream -   512 separation step -   513 effluent stream

While at least one exemplary embodiment has been presented in the foregoing detailed description, it should be appreciated that a vast number of variations exist. It should also be appreciated that the exemplary embodiment or exemplary embodiments are only examples, and are not intended to limit the scope, applicability, or configuration of the various embodiments in any way. Rather, the foregoing detailed description will provide those skilled in the art with a convenient road map for implementing an exemplary embodiment as contemplated herein. It being understood that various changes may be made in the function and arrangement of elements described in an exemplary embodiment without departing from the scope of the various embodiments as set forth in the appended claims. 

What is claimed is:
 1. Process for manufacturing ethyleneamine compounds selected from the group of ethyleneamines and hydroxyethylethyleneamines wherein the process comprises a first and a second reaction sequences, the first reaction sequence comprising the steps of: in an adduction step, providing a CO2 adduct of a starting compound comprising a —NH—CH2-CH2-NH— moiety or a —NH—CH2-CH2-OH moiety, or HO—CH2-CH2-OH, in a chain-extension step reacting a hydroxy-functional compound selected from ethanolamines and dihydroxyethane with an ethyleneamine compound, wherein at least part of a total of hydroxy-functional compounds and the ethyleneamine compound is provided in the form of a CO2 adduct, to form a CO2 adduct of a chain-extended ethyleneamine compound, in an elimination step converting the CO2 adduct of the chain-extended ethyleneamine compound to the corresponding product ethyleneamine compound by removal of the carbonyl group, and the second reaction sequence comprising the steps of: in a ethylenedichloride reaction step reacting ethylenedichloride with at least one compound selected from the group of ammonia, an ethyleneamine and/or an ethanolamine to form a hydrochloride salt of the ethyleneamine and/or the ethanolamine, in a caustic treatment step reacting a hydrochloride salt of the ethyleneamine or ethanolamine with a base to form an ethyleneamine compound and an inorganic chloride salt, in a salt separation step separating the inorganic chloride salt from the ethyleneamine compound, wherein the first reaction sequence and the second reaction sequence are connected in that at least one of the following takes place: effluent from a step in the first reaction sequence is provided as a starting material to a step in the second reaction sequence, effluent from a step in the second reaction sequence is provided as a starting material to a step in the first reaction sequence, a step of the first reaction sequence and a step of the second reaction sequence are combined, or effluent from a step in the first reaction sequence is combined with effluent from a step in the second reaction sequence.
 2. Process according to claim 1, wherein the ethyleneamine compound produced in the second reaction sequence is provided to one or more of the adduction step, the chain extension step, and the elimination step in the first reaction sequence.
 3. Process according to claim 1, wherein the CO2 adduct of the chain-extended ethyleneamine compound from the first reaction sequence is provided to the caustic treatment step in the second reaction sequence.
 4. Process according to claim 1, wherein the elimination step in the first reaction sequence comprises a caustic treatment, and a product of the caustic treatment in the first reaction sequence is combined with a product from the caustic treatment in the second reaction sequence, and the combined product is subjected to the salt separation step.
 5. Process according to claim 1, wherein the first reaction sequence produces first ethyleneamine reaction mixture, the second reaction sequence produces a second ethyleneamine reaction mixture, the first ethyleneamine reaction mixture is combined with the second ethyleneamine reaction mixture, and the combined product is subjected to a separation step.
 6. Process according to claim 1, wherein the CO2 adduct of the chain-extended ethyleneamine from the first reaction sequence is provided to the ethylenedichloride reaction step from the second reaction sequence.
 7. Process according to claim 1, wherein the CO2 adduct of the chain-extended ethyleneamine compound formed in the first reaction sequence is provided to the ethylenedichloride reaction step in the second reaction sequence, and the ethylenedichloride reaction step or the caustic treatment step in the second reaction sequence also produces a CO2 adduct that is provided to the elimination step in the first reaction sequence.
 8. Process according to claim 1, wherein the ethyleneamine compound produced in the second reaction sequence is provided to one or more of the adduction step, the chain extension step, or the elimination step in the first reaction sequence, and the ethyleneamine compound from the salt separation step in the second reaction sequence is provided to a fractionation step and fractionated into different ethyleneamine product fractions, wherein an ethyleneamine compound fraction is withdrawn from the elimination step in the first reaction sequence and provided to said fractionation step from the second reaction sequence and/or a product withdrawn from a step in the first reaction sequence is provided to the fractionation step in the second reaction sequence.
 9. Process according to claim 1, wherein the first reaction sequence and the second reaction sequence are connected in that an effluent from the chain extension step of the first reaction sequence and an effluent from the salt separation step in the second reaction sequence are provided to the same separation step.
 10. Process according to claim 2, wherein the CO2 adduct of the chain-extended ethyleneamine compound from the first reaction sequence is provided to the caustic treatment step in the second reaction sequence.
 11. Process according to claim 2, wherein the elimination step in the first reaction sequence comprises a caustic treatment, and a product of the caustic treatment in the first reaction sequence is combined with a product from the caustic treatment in the second reaction sequence, and the combined product is subjected to the salt separation step.
 12. Process according to claim 3, wherein the elimination step in the first reaction sequence comprises a caustic treatment, and a product of the caustic treatment in the first reaction sequence is combined with a product from the caustic treatment in the second reaction sequence, and the combined product is subjected to the salt separation step.
 13. Process according to claim 2, wherein the first reaction sequence produces a first ethyleneamine reaction mixture, the second reaction sequence produces a second ethyleneamine reaction mixture, the first ethyleneamine reaction mixture is combined with the second ethyleneamine reaction mixture, and the combined product is subjected to a separation step.
 14. Process according to claim 3, wherein the first reaction sequence produces a first ethyleneamine reaction mixture, the second reaction sequence produces a second ethyleneamine reaction mixture, the first ethyleneamine reaction mixture is combined with the second ethyleneamine reaction mixture, and the combined product is subjected to a separation step.
 15. Process according to claim 4, wherein the first reaction sequence produces a first ethyleneamine reaction mixture, the second reaction sequence produces a second ethyleneamine reaction mixture, the first ethyleneamine reaction mixture is combined with the second ethyleneamine reaction mixture, and the combined product is subjected to a separation step.
 16. Process according to claim 2, wherein the CO2 adduct of the chain-extended ethyleneamine from the first reaction sequence is provided to the ethylenedichloride reaction step from the second reaction sequence.
 17. Process according to claim 3, wherein the CO2 adduct of the chain-extended ethyleneamine from the first reaction sequence is provided to the ethylenedichloride reaction step from the second reaction sequence.
 18. Process according to claim 4, wherein the CO2 adduct of the chain-extended ethyleneamine from the first reaction sequence is provided to the ethylenedichloride reaction step from the second reaction sequence.
 19. Process according to claim 5, wherein the CO2 adduct of the chain-extended ethyleneamine from the first reaction sequence is provided to the ethylenedichloride reaction step from the second reaction sequence. 